R32 !Short name 75-10-5 !CAS number Difluoromethane !Full name CH2F2 !Chemical formula {CH2F2} HFC-32 !Synonym 52.024 !Molar mass [g/mol] 136.34 !Triple point temperature [K] 221.499 !Normal boiling point [K] 351.255 !Critical temperature [K] 5782. !Critical pressure [kPa] 8.1500846 !Critical density [mol/L] 0.2769 !Acentric factor 1.978 !Dipole moment [Debye]; Meyer & Morrison (1991) J. Chem. Eng. Data 36:409-413. IIR !Default reference state 10.0 !Version number 3252 !UN Number :UN: halocb !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 675. !GWP (IPCC 2007) :GWP: 36000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL: A2L !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/CH2F2/c2-1-3/h1H2 !Standard InChI String :InChi: RWRIWBAIICGTTQ-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: 7b05bb60 !Hash number from InChI Key :Hash: !The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the ! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended ! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to ! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary ! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and ! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the ! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the ! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations, ! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and ! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface ! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a ! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The ! end of the fluid file is marked with @END. Anything below that is ignored. ! compiled by M. McLinden, NIST Physical and Chemical Properties Division, Boulder, Colorado ! 11-01-95 MM, Original version. ! 11-13-97 MM, Enter thermal conductivity shape factor fitted to data. ! 11-01-99 EWL, Add Span 12 term short equation of state. ! 05-22-02 MLH, Change transport ref fluid to propane; refit coefficients; added kfit. ! 07-02-02 MLH, Add dedicated fit for thermal conductivity. ! 04-19-04 MLH, Update transport reference. ! 09-01-04 EWL, Add EOS of Astina and Sato. ! 03-23-05 EWL, Add PRT coefficient. ! 08-17-10 IDC, Add ancillary equations. ! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012). ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for R-32 of Tillner-Roth and Yokozeki (1997). :TRUECRITICALPOINT: 351.255 8.1500846 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1063/1.556002 ? ?``````````````````````````````````````````````````````````````````````````````` ?Tillner-Roth, R. and Yokozeki, A., ? "An International Standard Equation of State for Difluoromethane (R-32) ? for Temperatures from the Triple Point at 136.34 K to 435 K and Pressures ? up to 70 MPa," ? J. Phys. Chem. Ref. Data, 26(6):1273-1328, 1997. ? ?The estimated uncertainties are 0.05% for density, 0.02% for the vapor ? pressure, and 0.5%-1% for the heat capacity and speed of sound in the ? liquid phase. In the vapor phase, the uncertainty in the speed of sound ? is 0.02% ? !``````````````````````````````````````````````````````````````````````````````` 136.340 !Lower temperature limit [K] 435.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 27.4734 !Maximum density [mol/L] CPP !Pointer to Cp0 model 52.024 !Molar mass [g/mol] 136.34 !Triple point temperature [K] 0.0480 !Pressure at triple point [kPa] 27.4734 !Density at triple point [mol/L] 221.499 !Normal boiling point temperature [K] 0.2769 !Acentric factor 351.255 5782.0 8.1500846 !Tc [K], pc [kPa], rhoc [mol/L] 351.255 8.1500846 !Reducing parameters [K, mol/L] 8.314471 !Gas constant [J/mol-K] 19 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 1.046634 0.25 1. 0. !a(i),t(i),d(i),l(i) -0.5451165 1.0 2. 0. -0.002448595 -0.25 5. 0. -0.04877002 -1.0 1. 0. 0.03520158 2.0 1. 0. 0.00162275 2.0 3. 0. 0.2377225e-4 0.75 8. 0. 0.029149 0.25 4. 0. 0.003386203 18.0 4. 4. -0.004202444 26.0 4. 3. 0.0004782025 -1.0 8. 1. -0.005504323 25.0 3. 4. -0.02418396 1.75 5. 1. 0.4209034 4.0 1. 2. -0.4616537 5.0 1. 2. -1.200513 1.0 3. 1. -2.59155 1.5 1. 1. -1.400145 1.0 2. 1. 0.8263017 0.5 3. 1. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for R-32 of Tillner-Roth and Yokozeki (1997). ? ?``````````````````````````````````````````````````````````````````````````````` ?Tillner-Roth, R. and Yokozeki, A., 1997. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314471 !Reducing parameters for T, Cp0 1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.004486 0.0 1.160761 798.0 2.645151 4185.0 5.794987 1806.0 1.129475 11510.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-32 of Tillner-Roth and Yokozeki (1997). ? ?``````````````````````````````````````````````````````````````````````````````` ?Tillner-Roth, R. and Yokozeki, A., 1997. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 3.004486 1.0 !ai, ti for [ai*log(tau**ti)] terms -8.2581043885434511 0.0 !aj, ti for [ai*tau**ti] terms 6.3531025573429387 1.0 !aj, ti for [ai*tau**ti] terms 1.160761 798.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms 2.645151 4185.0 5.794987 1806.0 1.129475 11510.0 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FES !Helmholtz equation of state for R-32 of Span and Wagner (2003). ? ?``````````````````````````````````````````````````````````````````````````````` ?Span, R. and Wagner, W. ? "Equations of State for Technical Applications. III. Results for Polar Fluids," ? Int. J. Thermophys., 24(1):111-162, 2003. doi: 10.1023/A:1022362231796 ? ?The uncertainties of the equation of state are approximately 0.2% (to ? 0.5% at high pressures) in density, 1% (in the vapor phase) to 2% in ? heat capacity, 1% (in the vapor phase) to 2% in the speed of sound, and ? 0.2% in vapor pressure, except in the critical region. ? !``````````````````````````````````````````````````````````````````````````````` 136.34 !Lower temperature limit [K] 600.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 27.41 !Maximum density [mol/L] CPP !Pointer to Cp0 model 52.024 !Molar mass [g/mol] 136.34 !Triple point temperature [K] 0.047922 !Pressure at triple point [kPa] 27.41 !Density at triple point [mol/L] 221.49 !Normal boiling point temperature [K] 0.277 !Acentric factor 351.35 5795.0 8.2077503 !Tc [K], pc [kPa], rhoc [mol/L] 351.35 8.2077503 !Reducing parameters [K, mol/L] 8.31451 !Gas constant [J/mol-K] 12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.93080907 0.25 1. 0. !a(i),t(i),d(i),l(i) -2.4777491 1.25 1. 0. 0.41470439 1.5 1. 0. 0.054859755 0.25 3. 0. 0.00011475587 0.875 7. 0. -0.26225654 2.375 1. 1. 0.41118822 2.0 2. 1. 0.0034970526 2.125 5. 1. -0.096790506 3.5 1. 2. -0.1172821 6.5 1. 2. -0.04242838 4.75 4. 2. -0.012690083 12.5 2. 3. @EOS !---Equation of state--- BWR !MBWR equation of state for R-32 of Outcalt and McLinden (1995). ? ?``````````````````````````````````````````````````````````````````````````````` ?Outcalt, S.L. and McLinden, M.O., ? "Equations of state for the thermodynamic properties of R32 (difluoromethane) ? and R125 (pentafluoroethane)," ? Int. J. Thermophysics, 16:79-89, 1995. doi: 10.1007/BF01438959 ? !``````````````````````````````````````````````````````````````````````````````` 136.34 !Lower temperature limit [K] 500.0 !Upper temperature limit [K] 60000.0 !Upper pressure limit [kPa] 27.48 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 52.024 !Molar mass [g/mol] 136.34 !Triple point temperature [K] 0.0477 !Pressure at triple point [kPa] 27.48 !Density at triple point [mol/L] 221.494 !Normal boiling point temperature [K] 0.27680 !Acentric factor 351.35 5795.0 8.2078 !Tc [K], pc [kPa], rhoc [mol/L] 351.35 8.2078 !Reducing parameters [K, mol/L] 8.2078 !gamma 0.08314471 !Gas constant [L-bar/mol-K] 32 1 !Nterm, Ncoeff per term -0.000131275405202 0.899927934911 -28.1400805178 4360.91182784 -837235.280004 -0.782176408963e-6 -1.11226606825 539.331431878 288600.276863 -0.352264609289e-4 0.189661830119 -68.6549003993 -0.00349007064245 -0.0749983559476 -32.1524283063 0.00913057921906 -0.000171082181849 0.0503986984347 -0.000830354867752 -245522.676708 -10785905.6038 -4295.14279646 80872472.9567 -12.5945229993 -1057.35009761 -0.0904064745354 -1835.78733048 -0.000169690612464 0.0639250820631 -0.20492576744e-6 -0.00016562970087 -0.00932607493424 @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for R-32 of Outcalt and McLinden (1995). ? ?``````````````````````````````````````````````````````````````````````````````` ?Outcalt, S.L. and McLinden, M.O., ? "Equations of state for the thermodynamic properties of R32 (difluoromethane) ? and R125 (pentafluoroethane)," ? Int. J. Thermophysics, 16:79-89, 1995.doi: 10.1007/BF01438959 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 1.0 !Reducing parameters for T, Cp0 4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 36.79959 0.0 -0.06304821 1.0 0.0003757936 2.0 -3.219812e-7 3.0 @EOS !---Equation of state--- FE2 !Helmholtz equation of state for R-32 of Astina and Sato (2003). ? ?``````````````````````````````````````````````````````````````````````````````` ?Astina, I.M. and Sato, H. ? "A Rational Helmholtz Fundamental Equation of State for Difluoromethane with ? an Intermolecular Potential Background," ? Int. J. Thermophys., 24(4):963-990, 2003. doi: 10.1023/A:1025096716493 ? ?The estimated uncertainties of calculated properties from the equation of ? state are 0.07% in density for the liquid phase, 0.1% in pressure for the ? gaseous phase, 0.35% in pressure for the supercritical region, 0.07% in ? vapor pressure, 0.2% in saturated-liquid density, 0.7% in saturated-vapor ? density, 0.01% in speed of sound for the gaseous phase, 0.7% in speed of ? sound for the liquid phase, and 0.6% in isochoric specific heat for the ? liquid phase. ? !``````````````````````````````````````````````````````````````````````````````` 136.34 !Lower temperature limit [K] 450.0 !Upper temperature limit [K] 72000.0 !Upper pressure limit [kPa] 27.48 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 52.023 !Molar mass [g/mol] 136.34 !Triple point temperature [K] 0.0485 !Pressure at triple point [kPa] 27.47 !Density at triple point [mol/L] 221.488 !Normal boiling point temperature [K] 0.277 !Acentric factor 351.255 5782.0 8.150241 !Tc [K], pc [kPa], rhoc [mol/L] 351.255 8.150241 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 18 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 2.118688 0.5 1. 0. !a(i),t(i),d(i),l(i) -4.531096 1.125 1. 0. 1.442456 1.625 1. 0. 0.2053906 0.875 3. 0. -0.1311675 1.5 3. 0. 0.01022272 1.75 4. 0. 0.4873982 1.75 1. 1. -1.062213 2.75 1. 1. -0.004542051 0.25 5. 1. -6.933347e-4 3.75 5. 1. -0.03510307 1.0 6. 1. -0.05606161 6.5 1. 2. 0.08849625 2.5 2. 2. -0.01850758 7.5 5. 2. 0.007878071 7.5 6. 2. -0.03384115 11.0 2. 3. 1.641979e-4 16.0 2. 3. -0.001459172 13.0 8. 3. @AUX !---Auxiliary function for Cp0 CP2 !Ideal gas heat capacity function for R-32 of Astina and Sato (2003). ? ?``````````````````````````````````````````````````````````````````````````````` ?Astina, I.M. and Sato, H. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 351.255 8.314472 !Reducing parameters for T, Cp0 1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 3.99966 0.0 3.12115 1601.64447 0.9994221 760.3926 2.412721 4336.89982 3.055435 2064.64246 @AUX !---Auxiliary function for PH0 PH2 !Ideal gas Helmholtz form for R-32 of Astina and Sato (2003). ? ?``````````````````````````````````````````````````````````````````````````````` ?Astina, I.M. and Sato, H. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh 2.99966 1.0 !ai, ti for [ai*log(tau**ti)] terms -8.253834 0.0 !aj, ti for [ai*tau**ti] terms 6.351918 1.0 3.12115 -4.559777 !aj, ti for [ai*log(1-exp(ti*tau)] terms 0.9994221 -2.164788 2.412721 -12.34687 3.055435 -5.877902 @EOS !---Cubic equation of state--- PRT !Translated Peng-Robinson equation for R-32. ? ?``````````````````````````````````````````````````````````````````````````````` ?Volume translation of Peng Robinson EOS. ? !``````````````````````````````````````````````````````````````````````````````` 136.340 !Lower temperature limit [K] 435.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 27.4734 !Maximum density [mol/L] CPP !Pointer to Cp0 model 52.024 !Molar mass [g/mol] 0.2769 !Acentric factor 351.255 !Critical temperature [K] 5782.0 !Critical pressure [kPa] 8.1500846 !Critical density [mol/L] 8.314472 !Gas constant [J/mol-K] 1 !Number of parameters 0.00585 ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for R-32 of Perkins and Huber (2005) (unpublished) :DOI: 10.1021/je010001m ? ?``````````````````````````````````````````````````````````````````````````````` ?Unpublished; however the fit uses the functional form found in: ? Marsh, K., Perkins, R., and Ramires, M.L.V., ? "Measurement and Correlation of the Thermal Conductivity of Propane ? from 86 to 600 K at Pressures to 70 MPa," ? J. Chem. Eng. Data, 47(4):932-940, 2002. ? ?The estimated uncertainty of the correlation is 5%, except for the dilute gas and points ? approaching critical where the uncertainty rises to 10%. ? ?THERMAL CONDUCTIVITY ? Comparisons with specific data sets are given below. ? Le Neindre, B. and Garrabos, Y., "Measurement of Thermal Conductivity of HFC-32 (Difluoromethane) in the Temperature Range from 300 to 465 K at Pressures up to 50 MPa," Int. J. Thermophysics 22(3):701-722, 2001. ? Gao, X., Iojima, H., Nagasaka, Y., and Nagashima, A., "Thermal Conductivity of HFC-32 in the Liquid Phase," Paper C1c4, Proceedings 4th Asian Thermophysical Properties Conference, Tokyo, 1995. ? Ro, S.T., Kim, J.Y., and Kim, D.S., "Thermal Conductivity of R32 and its Mixture with R134a," Int. J. Thermophysics 16(5):1193-1201, 1995. doi: 10.1007/BF02081287 ? Tanaka, Y., Matsuo, S., and Taya, S., "Gaseous Thermal Conductivity of Difluoromethane (HFC-32), Pentafluoroethane (HFC), and Their Mixtures," Int. J. Thermophys., 16(1):121-131, 1995. doi: 10.1007/BF01438963 ? Papadaki, M. and Wakeham, W.A., "Thermal Conductivity of R32 and R125 in the Liquid Phase at the Saturation Vapor Pressure," Int. J. Thermophys., 14(6):1215-1220, 1993. doi: 10.1007/BF02431285 ? Assael, M.J. and Karagiannidis, L., "Measurements of the Thermal Conductivity of Liquid R32, R124, R125 and R141b," Int. J. Thermophys., 16(4):851-865, 1995. doi: 10.1007/BF02093468 ? Gross, U. and Song, Y.W., "Thermal Conductivities of New Refrigerants R125 and R32 Measured by the Transient Hot-Wire Method," Int. J. Thermophys., 17(3):607-619, 1996. doi: 10.1007/BF01441507 ? Yata, J., Hori, M., Kobayashi, K., and Minimiyama, T., "Thermal Conductivity of Alternative Refrigerants in the Liquid Phase," Int. J. Thermophys., 17(3):561-571, 1996. doi: 10.1007/BF01441503 ? Perkins, R.A., 2002, unpublished data. 325 Broadway, Boulder, CO 80305, perkins@boulder.nist.gov ? Average absolute deviations of the fit from the experimental data are: ? Le Neindre: 2.13%; Gao: 1.66%; Ro: 2.26%; Tanaka: 2.85%; Papadaki: 3.12%; ? Assael: 2.90%; Gross: 3.85%; Yata: 2.86%; Perkins: 1.69%. ? Overall: 1.93%. ? !``````````````````````````````````````````````````````````````````````````````` 136.340 !Lower temperature limit [K] 435.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 27.4734 !Maximum density [mol/L] 3 0 !# terms for dilute gas function: numerator, denominator 351.255 1.0 !Reducing parameters for T, tcx 0.0106548 0. !Coefficient, power in T -0.0194174 1. 0.0254295 2. 10 0 !# terms for background gas function: numerator, denominator 351.255 8.1500846 1. !Reducing parameters for T, rho, tcx 0.0221878 0. 1. 0. !Coefficient, powers of T, rho, spare for future use -0.0215336 1. 1. 0. 0.283523 0. 2. 0. -0.169164 1. 2. 0. -0.297237 0. 3. 0. 0.191614 1. 3. 0. 0.105727 0. 4. 0. -0.0665397 1. 4. 0. -0.0123172 0. 5. 0. 0.00766378 1. 5. 0. TK3 !Pointer to critical enhancement auxiliary function #AUX !---Auxiliary function for the thermal conductivity critical enhancement TK3 !Simplified thermal conductivity critical enhancement for R-32 of Olchowy and Sengers (1989). ? ?``````````````````````````````````````````````````````````````````````````````` ?Olchowy, G.A. and Sengers, J.V., ? "A Simplified Representation for the Thermal Conductivity of Fluids in the Critical Region," ? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 9 0 0 0 !# terms: CO2-terms, spare, spare, spare 1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)] 0.63 !Nu (universal exponent) 1.239 !Gamma (universal exponent) 1.03 !R0 (universal amplitude) 0.063 !Z (universal exponent--not used for t.c., only viscosity) 1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1) 0.194e-9 !Xi0 (amplitude) [m] 0.0496 !Gam0 (amplitude) [-] 5.582925e-10 !Qd_inverse (modified effective cutoff parameter) [m]; fitted to data 526.8825 !Tref (reference temperature)=1.5*Tc [K] ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (Propane reference); fitted to data for R-32. :DOI: 10.1021/ie0300880 ? ?``````````````````````````````````````````````````````````````````````````````` ?Unpublished; uses method described in the following reference: ?Huber, M.L., Laesecke, A., and Perkins, R.A. ? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including ? a New Correlation for the Viscosity of R134a," ? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880 ? ?THERMAL CONDUCTIVITY ? The ECS parameters for thermal conductivity were based in part on the data of: ? Le Neindre, B. and Garrabos, Y. (2001) "Measurement of Thermal Conductivity of HFC-32 (Difluoromethane) in the temperature range from 300 to 465 K at pressures up to 50 MPa", Int. J. Thermophysics 22(3): 701-722. doi: 10.1023/A:1010766730306 ? Gao, X., Iojima, H., Nagasaka, Y. and Nagashima, A. (1995). "Thermal conductivity of HFC-32 in the liquid phase", Paper C1c4, Proceedings 4th Asian Thermophysical Properties Conference, Tokyo. ? Perkins, R.A.,(2002) personal communication. 325 Broadway, Boulder, CO 80305, perkins@boulder.nist.gov ? Average absolute deviations of the fit from the experimental data are: ? LeNeindre: 2.75%; Gao: 3.92%; Perkins: 4.81% Overall: 4.23% ? ?VISCOSITY ? The ECS parameters for viscosity were based in part on the data of: ? Laesecke, A., Luddecke, T.O.D., Hafer, R.F. and Morris, D.J. (1999). Viscosity measurements of ammonia, R32, and R134a. Vapor buoyancy and radial acceleration in capillary viscometers, Int. J. Thermophys. 20(2):401-434. doi: 10.1023/A:1022644718603 ? Bivens, D.B., Yokozeki, A., Geller, V.Z., and Paulaitis, M.E. (1993). Transport properties and heat transfer of alternatives for R502 and R22. ASHRAE/NIST Refrigerants Conference, August 19-20, Gaithersburg, MD, 73-84. ? Shibasaki-Kitakawa, N., Takahashi, M., Yokoyama, C., and Takahashi, S., (1995). Gas viscosity of difluoromethane from 298.15 K to 423.15 K and up to 10 MPa. J. Chem. Eng. Data, 40:900-902. doi: 10.1021/je00020a036 ? Oliveira, C. M. B. P., and Wakeham, W. A. (1993). "The viscosity of R32 and R125 at saturation", Int. J. Thermophys.14: 1131-43.doi: 10.1007/BF02431279 ? Average absolute deviations of the fit from the experimental data are: ? Laesecke: 0.66; Bivens: 4.43%; Takahashi: 2.65%; Oliveira: 2.80%; Overall: 2.17% ? ?The Lennard-Jones parameters were based on the low-density viscosity data of Takahashi. ? !``````````````````````````````````````````````````````````````````````````````` 136.34 !Lower temperature limit [K] 435.0 !Upper temperature limit [K] 70000.0 !Upper pressure limit [kPa] 27.4734 !Maximum density [mol/L] FEQ PROPANE.FLD VS1 !Model for reference fluid viscosity TC1 !Model for reference fluid thermal conductivity NUL !Large molecule identifier 1 !Lennard-Jones flag (0 or 1) (0 => use estimates) 0.4098 !Lennard-Jones coefficient sigma [nm] for ECS method 289.65 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method 2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 4.36654e-4 0. 0. 0. !Coefficient, power of T, spare1, spare2 1.78134e-6 1. 0. 0. !Coefficient, power of Tr, power of Dr, spare 2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 0.795399 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare 0.0542658 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare 2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2 1.29424 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.0924549 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare TK3 !Pointer to critical enhancement auxiliary function ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for R-32 of Mulero et al. (2012). :DOI: 10.1063/1.4768782 ? ?``````````````````````````````````````````````````````````````````````````````` ?Mulero, A., Cachadiņa, I., and Parra, M.I., ? "Recommended Correlations for the Surface Tension of Common Fluids," ? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 !Number of terms in surface tension model 351.255 !Critical temperature used in fit (dummy) 0.07147 1.246 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-32 of Cullimore (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Cullimore, I.D., 2010. ? ?Functional Form: P=Pc*EXP[SUM(Ni*Theta^ti)*Tc/T] where Theta=1-T/Tc, Tc and Pc ? are the reducing parameters below, which are followed by rows containing Ni and ti. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 351.255 5782.0 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -7.4883 1.0 1.9697 1.5 -1.7496 2.2 -4.0224 4.8 1.5209 6.2 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-32 of Cullimore (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Cullimore, I.D., 2010. ? ?Functional Form: D=Dc*[1+SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are ? the reducing parameters below, which are followed by rows containing Ni and ti. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 351.255 8.1500846 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation 1.2584 0.27 4.6410 0.8 -5.4870 1.1 3.3115 1.5 -0.61370 1.8 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-32 of Cullimore (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?Cullimore, I.D., 2010. ? ?Functional Form: D=Dc*EXP[SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are ? the reducing parameters below, which are followed by rows containing Ni and ti. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 351.255 8.1500846 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -2.2002 0.336 -5.9720 0.98 -14.571 2.7 -42.598 5.7 4.2686 6.5 -73.373 11.0 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890